EP0059282A2 - Méthode pour contrôler la distribution au point d'ébullition du produit de liquéfaction du charbon - Google Patents

Méthode pour contrôler la distribution au point d'ébullition du produit de liquéfaction du charbon Download PDF

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Publication number
EP0059282A2
EP0059282A2 EP81303679A EP81303679A EP0059282A2 EP 0059282 A2 EP0059282 A2 EP 0059282A2 EP 81303679 A EP81303679 A EP 81303679A EP 81303679 A EP81303679 A EP 81303679A EP 0059282 A2 EP0059282 A2 EP 0059282A2
Authority
EP
European Patent Office
Prior art keywords
distillate
light
heavy
ratio
heavy distillate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP81303679A
Other languages
German (de)
English (en)
Other versions
EP0059282A3 (en
EP0059282B1 (fr
Inventor
Raymond Paul Anderson
Charles Hubert Wright
David Keith Schmalzer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
RAG AG
Mitsui Src Development Co Ltd
Pittsburgh and Midway Coal Mining Co
Original Assignee
Ruhrkohle AG
Mitsui Src Development Co Ltd
Pittsburgh and Midway Coal Mining Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ruhrkohle AG, Mitsui Src Development Co Ltd, Pittsburgh and Midway Coal Mining Co filed Critical Ruhrkohle AG
Publication of EP0059282A2 publication Critical patent/EP0059282A2/fr
Publication of EP0059282A3 publication Critical patent/EP0059282A3/en
Application granted granted Critical
Publication of EP0059282B1 publication Critical patent/EP0059282B1/fr
Expired legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/008—Controlling or regulating of liquefaction processes

Definitions

  • This invention relates to a method of controlling the boiling point distribution of the liquid product of a coal liquefaction process wherein a mineral-containing feed coal is dissolved in a solvent and hydrocracked. More particularly, this invention relates to a method for controlling the relative ratio of heavy distillate to light distillate produced in a coal liquefaction process by continuously controlling the ratio of heavy distillate to light distillate fed to the liquefaction zone.
  • U.S. Patent No. 4,152,244 to Raichle et al discloses the use of a mixture of middle oil (200°-325°C) and heavy oil (325°-450°C) as a slurry liquid in a coal hydrogenation process wherein a portion of the recycled oil mixture must be hydrogenated.
  • the patent does not teach that the concentration of a particular distillate fraction produced in a coal liquefaction process can be controlled by controlling the concentration of such fraction relative to another fraction present as solvent liquid fed to a coal liquefaction reaction.
  • the production of heavy distillate is maximized by controlling the ratio of light distillate to heavy distillate in the feed slurry to a value greater than 0.4:1, preferably in the range of between about 0.4:1 to about 4:1, most preferably between about 0.6:1 to about 3:1 on a weight basis.
  • the conditions in the dissolver include a temperature in the range of 750° to 900°F (399° to 482°C), preferably 820° to 870°F (438° to 466°C) and a residence time of 0.1 to 4.0 hours, preferably 0.2 to 2 hours.
  • the pressure is in the range of 1,000 to 4,000 psi and is'preferably 1,500 to 3,000 psi (70 to 280 kg/cm 2 , preferably 105 to 210 kg/cm 2 ).
  • a portion of the purified gas is passed through line 42 for further processing in cryogenic unit 44 for removal of much of the methane and ethane as pipeline gas which passes through line 46 and for the removal of propane and butane as LPG which passes through line 48.
  • the purified hydrogen in line 50 is blended with the remaining gas from the acid gas treating step in line 52 and comprises the recycle hydrogen for the process.
  • fractionator 36 the slurry product is distilled at atmospheric pressure to remove an overhead naphtha stream through line 62, a 350°F (177°C) to 600°F (316°C) light distillate stream through line 64 and a bottoms stream through line 66.
  • the bottoms stream in line 66 passes to vacuum distillation tower 68.
  • the temperature of the feed to the fractionation system is normally maintained at a sufficiently high level that no additional preheating is needed, other than for start-up operations..
  • a heavy distillate stream comprising 600°F (316°C) to 800°F (427°C) material is withdrawn from the vacuum tower through line 70.
  • the combination of the light and heavy distillates in lines 64 and 70 makes up the major fuel oil product of the process.
  • the relative yields of the light distillate and heavy distillate in lines 64 and 70, respectively, can be controlled by controlling the concentration of light distillate and heavy distillate in the feed slurry in process line 16.
  • Control of the concentration of light and heavy distillate in the feed slurry can be accomplished by any suitable means.
  • concentration is controlled by automatically and continuously controlling the amount of light and heavy distillate fractions which are passed to line 73 for recycle to the slurry mixing tank by means of line 14.
  • concentration of the light distillate in line 73 is thus controlled by automatically and continuously controlling the rate of light distillate introduced into line 73 by means of three-way valve 76 and line 78.
  • the concentration of heavy distillate in line 73 is controlled by automatically and continuously controlling the rate of heavy distillate introduced into line 73 by means of three-way valve 80 and line 82.
  • the amount of light distillate passing through line 64 is automatically and continuously monitored by measuring device 84, and the resulting signal . is transmitted by means of output line 86 to the automatic control instrument 88.
  • the amount of heavy distillate passing through line 72 is monitored by measuring device 90 and the signal is automatically and continuously transmitted by output line 92 to automatic control instrument 88.
  • the automatic control instrument regulates the amount of light distillate recycled by controlling automatic valve 76 by means of input line 94.
  • the amount of heavy distillate that is recycled is controlled by the automatic control instrument 88 by regulating the operation of automatic valve 80 by means of input line 96.
  • Automatic control instrument 88 and flow measuring sensors 84 and 90 can be of conventional design well known to the art, and can be, for example, differential pressure, thermal or sonic type flow measuring devices.
  • the ratio of heavy distillate to light distillate in the feed slurry for example, to between: about 5:1 to about 15:1, the ratio of heavy distillate to light distillate withdrawn as a fuel oil product by means of lines 72 and 64, respectively, can be controlled within a range of between about 0.2:1 to about 1:1.
  • the bottoms from vacuum tower 68 consisting of all the normally solid dissolved coal, undissolved organic matter and mineral matter of the process, but essentially without any distillate liquid or hydrocarbon gases is discharged by means of line 74, and may be processed as desired.
  • such stream may be passed to a partial oxidation gasifier to produce hydrogen for the process in the manner described in U.S. Patent No. 4,159,236 to Schmid, the disclosure of which is hereby incorporated by reference.
  • the process as depicted in FIG. 1 does not employ any hydrogenation reaction zone involving either catalytic or non-catalytic hydrogenation downstream from dissolver 26 prior to separation of the liquid into light and heavy distillate fractions in fractionator 36 and vacuum tower 68.
  • the recycle light distillate and heavy distillate are unhydr6genated.
  • Tests 4-6 were conducted using a Pittsburgh seam coal from a different location having a slightly higher ash content of 11.7 weight percent on a weight basis.
  • a feed slurry is prepared for each test by mixing pulverized coal with liquid solvent and a recycle slurry containing liquid solvent, normally solid dissolved coal and catalytic mineral residue.
  • the feed slurry was formulated such that the ratio of the light oil fraction (approximate boiling range 193°-282°C, 380'-540°F) to heavy oil fraction (approximate boiling range 282°-482°C, 540 *- 900°F) in the liquid solvent was varied, while the total amount of the two oil fractions remained relatively constant, varying only from 34.2 to 36.8 weight percent of the total feed slurry composition.
  • the coal concentration in the feed slurry was 30 weight percent and the pressure was 1800 psig (126 kg/cm 2 ) using an average dissolver temperature of 455°-457°C (851°-855°F).
  • the hydrogen feed rate was 49-72 MSCF/ton of coal (1.52-2.23 M 3 /kg).
  • the coal feed rate was 21.0-21.5 Ib/hr/ft3, which corresponds to a nominal slurry residence time of 1.0-1.02 hour.
  • the composition of the feed slurry was adjusted in part by varying the temperature of the high pressure separator (350-390°C) and the distillation column, but more importantly, by the slurry formulation procedure.
  • Light distillate and heavy distillate were collected separately.
  • the light distillate has an approximate boiling range of 193°C, 380°F, to 282°C, 540°F (atmospheric boiling point corrected from actual cut point of 108°C at 2 mmHg).
  • the heavy distillate has an approximate boiling range of 282°C, 548 * F, to 482°C, 900°F (atmospheric boiling point corrected from actual cut point of 270°C at 2 mmHg).
  • the ratio of light distillate and heavy distillate used in slurry formulation was adjusted to provide the desired feed slurry composition as shown in Table I above. The results of the various tests are set forth in Table II below:
  • FIGS. 2 and 3 show the effect of recycle distillate composition upon product distillate composition. Since the concentration of total distillate (light distillate plus heavy distillate) is approximately the same for all . experiments, the concentration of light or heavy distillate is also a measure of the ratio of light distillate to heavy distillate.
  • the actual data points shown in FIGS. 2 and 3 were taken from Tables 1 and 2.
  • the solid line shown in FIG. 2 was obtained by mathematical correlation based upon a large number of experiments carried out under various conditions and indicate little or no effect of re- cycle distillate composition upon predicted yields of light and heavy distillates. The actual data points show, unpredictably, that the yield of light distillate increases as the concentration of heavy distillate (shown as a decrease in light distillate concentration) in the slurry feed is increased.
  • the solid line in. FIG. 3 obtained by mathematical correlation predicts that the concentrations of light and heavy fuel oil, respectively, in the recycle distillate have little or no effect upon the relative yields of light and heavy distillate.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP81303679A 1981-03-04 1981-08-13 Méthode pour contrôler la distribution au point d'ébullition du produit de liquéfaction du charbon Expired EP0059282B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US06/237,762 US4364817A (en) 1981-03-04 1981-03-04 Method for controlling boiling point distribution of coal liquefaction oil product
US237762 1981-03-04

Publications (3)

Publication Number Publication Date
EP0059282A2 true EP0059282A2 (fr) 1982-09-08
EP0059282A3 EP0059282A3 (en) 1983-10-05
EP0059282B1 EP0059282B1 (fr) 1987-02-04

Family

ID=22895056

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81303679A Expired EP0059282B1 (fr) 1981-03-04 1981-08-13 Méthode pour contrôler la distribution au point d'ébullition du produit de liquéfaction du charbon

Country Status (11)

Country Link
US (1) US4364817A (fr)
EP (1) EP0059282B1 (fr)
AU (1) AU548626B2 (fr)
BR (1) BR8108982A (fr)
CA (1) CA1174624A (fr)
DE (1) DE3175904D1 (fr)
ES (1) ES8302073A1 (fr)
IL (1) IL63395A0 (fr)
PL (1) PL233592A1 (fr)
WO (1) WO1982003083A1 (fr)
ZA (1) ZA815626B (fr)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3042984C2 (de) * 1980-11-14 1986-06-26 Saarbergwerke AG, 6600 Saarbrücken Verfahren zum Hydrieren von Kohle
JPS59109588A (ja) * 1982-12-15 1984-06-25 Kobe Steel Ltd 褐炭の液化方法
US4879021A (en) * 1983-03-07 1989-11-07 Hri, Inc. Hydrogenation of coal and subsequent liquefaction of hydrogenated undissolved coal
US4569749A (en) * 1984-08-20 1986-02-11 Gulf Research & Development Company Coal liquefaction process
US4541916A (en) * 1984-10-18 1985-09-17 Gulf Research & Development Corporation Coal liquefaction process using low grade crude oil
US4874506A (en) * 1986-06-18 1989-10-17 Hri, Inc. Catalytic two-stage coal hydrogenation process using extinction recycle of heavy liquid fraction
CA2022721C (fr) * 1990-08-03 1999-10-26 Teresa Ignasiak Methode de conversion d'huile lourde deposee sur fines de charbon en une huile distillable selon un procede a faible intensite
US5733529A (en) * 1995-06-05 1998-03-31 Whitehill Oral Technologies, Inc. Ultramulsion based antigingivitis toothpaste compositions
US5730967A (en) * 1995-06-05 1998-03-24 Whitehill Oral Technologies, Inc. Ultramulsion based skin care compositions
US5733536A (en) * 1995-06-05 1998-03-31 Whitehill Oral Technologies, Inc. Ultramulsion based hair care compositions
US10400108B2 (en) * 2016-04-29 2019-09-03 Axens Carbon black feedstock from direct coal liquefaction

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3075912A (en) * 1958-09-18 1963-01-29 Texaco Inc Hydroconversion of solid carbonaceous materials
US4045329A (en) * 1974-01-21 1977-08-30 Hydrocarbon Research, Inc. Coal hydrogenation with selective recycle of liquid to reactor
US4159238A (en) * 1978-05-12 1979-06-26 Gulf Oil Corporation Integrated coal liquefaction-gasification process

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3790467A (en) * 1970-08-27 1974-02-05 Exxon Research Engineering Co Coal liquefaction solids removal
US3726785A (en) * 1971-03-03 1973-04-10 Exxon Research Engineering Co Coal liquefaction using high and low boiling solvents
DE2654635B2 (de) * 1976-12-02 1979-07-12 Ludwig Dr. 6703 Limburgerhof Raichle Verfahren zur kontinuierlichen Herstellung von Kohlenwasserstoffölen aus Kohle durch spaltende Druckhydrierung
US4159236A (en) * 1978-05-12 1979-06-26 Gulf Oil Corporation Method for combining coal liquefaction and gasification processes
US4159237A (en) * 1978-05-12 1979-06-26 Gulf Oil Corporation Coal liquefaction process employing fuel from a combined gasifier
US4211631A (en) * 1978-07-03 1980-07-08 Gulf Research And Development Company Coal liquefaction process employing multiple recycle streams
US4222845A (en) * 1978-12-13 1980-09-16 Gulf Oil Corporation Integrated coal liquefaction-gasification-naphtha reforming process
US4230556A (en) * 1978-12-15 1980-10-28 Gulf Oil Corporation Integrated coal liquefaction-gasification process
US4255248A (en) * 1979-09-07 1981-03-10 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent having a low heptane-insolubiles content

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3075912A (en) * 1958-09-18 1963-01-29 Texaco Inc Hydroconversion of solid carbonaceous materials
US4045329A (en) * 1974-01-21 1977-08-30 Hydrocarbon Research, Inc. Coal hydrogenation with selective recycle of liquid to reactor
US4159238A (en) * 1978-05-12 1979-06-26 Gulf Oil Corporation Integrated coal liquefaction-gasification process

Also Published As

Publication number Publication date
US4364817A (en) 1982-12-21
ES504886A0 (es) 1983-01-01
AU548626B2 (en) 1985-12-19
CA1174624A (fr) 1984-09-18
PL233592A1 (fr) 1982-09-13
AU7453881A (en) 1982-09-28
WO1982003083A1 (fr) 1982-09-16
EP0059282A3 (en) 1983-10-05
BR8108982A (pt) 1983-01-25
EP0059282B1 (fr) 1987-02-04
IL63395A0 (en) 1981-10-30
DE3175904D1 (en) 1987-03-12
ES8302073A1 (es) 1983-01-01
ZA815626B (en) 1982-08-25

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